EP0335071A1 - Procédé et installation de transport pneumatique d'un combustible finement granulé jusqu'à pulvérulent dans un réacteur de gazéification sous pression élevée - Google Patents

Procédé et installation de transport pneumatique d'un combustible finement granulé jusqu'à pulvérulent dans un réacteur de gazéification sous pression élevée Download PDF

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Publication number
EP0335071A1
EP0335071A1 EP89101155A EP89101155A EP0335071A1 EP 0335071 A1 EP0335071 A1 EP 0335071A1 EP 89101155 A EP89101155 A EP 89101155A EP 89101155 A EP89101155 A EP 89101155A EP 0335071 A1 EP0335071 A1 EP 0335071A1
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EP
European Patent Office
Prior art keywords
fuel
gas
gasification reactor
container
pressure pot
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP89101155A
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German (de)
English (en)
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EP0335071B1 (fr
Inventor
Hans-Richard Baumann
Hans-Reiner Schweimanns
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Krupp Koppers GmbH
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Krupp Koppers GmbH
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Filing date
Publication date
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Publication of EP0335071A1 publication Critical patent/EP0335071A1/fr
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Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/50—Fuel charging devices
    • C10J3/506—Fuel charging devices for entrained flow gasifiers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/466—Entrained flow processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/723—Controlling or regulating the gasification process
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C10K1/024—Dust removal by filtration
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C10K1/026—Dust removal by centrifugal forces
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0956—Air or oxygen enriched air
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/12—Heating the gasifier
    • C10J2300/1223—Heating the gasifier by burners
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]

Definitions

  • the invention relates to a method and a device for the pneumatic conveying of a fine-grained to dusty fuel from a pressurized storage bunker into a pressurized gasification reactor in which the fuel is gasified in the entrained flow with oxygen and / or air and possibly water vapor, the Fuel is conveyed from the storage bunker into the gasification reactor by means of a pressure pot conveyor via an allotment container.
  • the invention is therefore based on the object of improving the method of the type mentioned in such a way that it is suitable for use in large-scale plants whose gasification reactors have two or more burners.
  • the process conditions are to be designed at the same time in such a way that a uniform and continuous fuel supply to all burners is ensured under optimal conditions.
  • the method of the type mentioned at the outset which is used to achieve this object is thus known is characterized in that all the burners of a gasification reactor are supplied via a central supply container, the fuel supply to the supply container being adapted to the fuel removal and being carried out continuously via at least two pressure pot conveyors which are filled and emptied at different times.
  • the method of operation according to the invention ensures that a stable level of the fuel bed is established in the central feed tank, which serves to supply all burners, and thus fluctuations due to different gas flow through the fuel bed in the feed tank, which would impair the uniformity of the fuel delivery to the burners, are avoided .
  • the arrangement of at least two pressure pot conveyors on the supply container, which are alternately filled and emptied, ensures a continuous supply of fuel to the supply container and thus to the downstream burner.
  • the combustible gas serving as the conveying gas can either be the CO2-free synthesis gas generated in the process or a residual gas or flash gas from the gas purification stages of the synthesis gas system.
  • the residual gas containing SO2 from the Claus plant can be used and thus be fed to a treatment in the gasification reactor which is environmentally friendly.
  • the raw gas generated during gasification is used to produce a fuel gas, e.g. for a gas-steam turbine power plant, then a certain proportion of inert gas in the raw gas produced during the gasification is not critical.
  • an inert gas e.g. impure nitrogen with a maximum oxygen content of 6% and / or CO2 can be used as the conveying gas.
  • the coal dust coming from the storage bunker of the processing plant and under normal pressure is transported via line 1 into the cyclone filter 2a by means of CO2 as an inert conveying gas.
  • the coal dust is separated from the conveying gas and this is removed in the cleaned state via line 22.
  • approx. 50 Nm3 CO2 per ton of coal dust are required for transport. Since both the cyclone filter 2a and the associated pressure pot conveyor 3a are under normal pressure during the filling process, the pulverized coal enters the line 4 under the influence of gravity Pressure pot conveyor 3a.
  • the coal dust supply via the line 4 is interrupted by closing the valve 5 which is arranged in the line 4.
  • CO2 is pressed into the pressure pot conveyor 3a until a pressure has set in it, which is usually 0.5 to 2 bar above the operating pressure prevailing in the supply container 8.
  • a pressure of 31 bar prevails in the pressure pot conveyor 3a, while the pressure in the distribution container 8 is approximately 30 bar.
  • lines 11 and 12 branch off, through which additional CO2 can be introduced in the area of the funnel-shaped taper via uniformly distributed nozzles into the pressure pot conveyor 3a.
  • This additional CO2 supply serves primarily to adjust the flow rate density of the coal dust drawn off via the delivery line 10 according to the invention so that it is of the order of 60-90% of the bulk density of the coal dust used.
  • this gas introduction prevents bridging when the coal dust escapes from the pressure pot conveyor 3a.
  • the CO2 supply via lines 11 and 12 is limited so that a fluidized bed-like loosening of the coal dust in the pressure pot conveyor 3a is avoided.
  • the line 13 opens into the delivery line 10, through which purge gas can be blown into the delivery line 10 if necessary, around this line rinse after emptying the pressure pot conveyor 3a and closing the valve 9.
  • a partial stream of the synthesis gas generated can be used as the purge gas.
  • the supply of CO2 via lines 7, 11 and 12 is interrupted and the pressure pot conveyor 3a is expanded in two phases.
  • the CO2 is introduced via line 14 into the buffer tank 15.
  • the CO2 collected in the buffer tank 15 is drawn off via the line 16 and can be reused for the pneumatic conveying of the coal dust to the cyclone filter 2a.
  • This CO2 covers about 75% of the need.
  • the valve 17a is closed while the valves 18 and 19 are open, so that the slightly contaminated CO2 is introduced via the lines 20 and 21 into the cyclone filter 2a. From this, the CO2 is discharged into the atmosphere via line 22 after the entrained coal dust has been separated off.
  • the supply container 8 is assigned a further pressure pot conveyor 3b with the associated cyclone filter 2b, one pressure pot conveyor being alternately filled while the other is emptied.
  • the supply container 8 can be continuously supplied with coal dust, the supply of coal dust to the supply container 8 being adapted to the extraction of coal dust to such an extent that the level of the coal dust fill in the distribution container 8 has only very slight fluctuations. The range of these fluctuations is hatched in the illustration.
  • the lines and valves assigned to the pressure pot conveyor 3b and the cyclone filter 2b each have the same reference numerals as the corresponding lines and valves on the pressure pot conveyor 3a and on the cyclone filter 2a. Since these lines and valves have the same function, their mode of operation need not be discussed again here.
  • the pressure pot conveyors 3a and 3b are arranged next to and not vertically above the feed container 8 and are only connected to it via the delivery line 10. This enables on the one hand a compact design of the entire system and on the other hand prevents the fuel delivery to the feed container 8 via the delivery line 10 under the influence of gravity, which would impair its controllability.
  • the design of the pressure pot conveyors 3a and 3b takes place taking into account the generally known and the data determined specifically for the fuel used in such a way that a complete and uniform emptying of the pressure pot conveyors via the delivery line 10 is ensured without the additional addition of conveying gas into this line.
  • the emptying of the pressure pot conveyors 3a and 3b is alternately initiated when a minimum permissible fuel level has been reached in the supply container 8.
  • This minimum fill level is identified in the figure by the lower boundary line of the hatched area in the distribution container 8.
  • the mass flow during emptying depends on the setting th and automatically readjusted differential pressure between the pressure pot conveyors 3a and 3b and the supply container 8.
  • This differential pressure is determined by the differential pressure meters 23a and 23b, which via the pulse lines 24a and 24b with the pressure pot conveyors 3a and 3b and via the pulse lines 25a and 25b with the supply container 8 are connected and act on valves 6a or 6b and 17a or 17b via differential pressure regulators.
  • the differential pressure control works as follows:
  • the fuel mass flow in the lines 38, 39, 40 and 41 leading from the supply container 8 to the gasification reactor 27 is determined and added to a total fuel mass flow. Using suitable measuring devices in lines 38, 39, 40 and 41, this mass flow is set to full load in accordance with the design of the gasification reactor 27. This mass flow can only be maintained if a constant differential pressure is regulated and maintained between the feed container 8 and the gasification reactor 27.
  • This differential pressure is determined by the differential pressure meter 44, which is connected to the feed tank 8 via the pulse line 45 and to the gasification reactor 27 via the pulse line 46.
  • the differential pressure meter 44 acts on the control valve 47 for the gas supply to the supply container 8 via the line 33 and on the control valve 49 for the gas discharge from the supply container 8.
  • the setpoint of the differential pressure meter 44 can be changed automatically or by manual intervention.
  • the function of the differential pressure meters 23a and 23b already described above is comparable to the function of the differential pressure meter 44.
  • the setpoint of the differential pressure meters 23a and 23b is automatically adjusted in relation to the setpoint of the differential pressure meter 44.
  • the fuel mass flow to the gasification reactor 27 is thus the reference variable for the subsequent delivery of fuel from the pressure pot conveyors 3a and 3b to the supply container 8. Since the delivery line 10 from the pressure pot conveyor 3a to the supply container 8 can have a different pressure loss than the corresponding line from the pressure pot conveyor 3b to the supply container 8, the respective differential pressures must be determined and controlled by two separate differential pressure meters 23a and 23b.
  • the setpoint of the differential pressure meters 23a and 23b can also be changed directly in relation to the total fuel mass flow in the lines leading to the gasification reactor 27. Since the determination of the mass flows in the lines leading to the gasification reactor 27 and the determination of the total mass flow are not the subject of the present invention, no further explanation is given here.
  • the fuel mass flow rate set by the differential pressure control should be able to fluctuate between 100% and 25%, so that an almost constant fill level in the supply container 8 is guaranteed under all operating conditions.
  • the allocation container 8 serves, as has already been established, for the central fuel supply to all burners of the gasification reactor 27.
  • a partial flow of the synthesis gas (CO + H2) is used as the conveying gas for the transport of the coal dust from the feed container 8 to the burners in the gasification reactor 27.
  • This partial flow is withdrawn from the gas treatment plant 29 via the line 30 and brought to the required pressure in the compressor 31.
  • the synthesis gas then passes via line 32 to lines 33 and 34, via which it is introduced into the area of the funnel-shaped taper of the supply container 8 via uniformly distributed nozzles therein.
  • the synthesis gas drawn off via the line 32 is heated in the steam-heated heat exchanger 35 until it has at least the temperature of the coal dust in the feed container 8.
  • the coal dust is withdrawn via line 36, the gas supply via lines 33 and 34 being adjusted so that bridging of the coal dust is avoided and the flow rate density in line 36 and the downstream lines leading to the burners of the order of magnitude is 60 - 90% of the bulk density of the coal dust used.
  • the coal dust reaches the distributor 37 via the line 36, from where it is supplied to the four burners of the gasification reactor 37, which are uniformly distributed via the lines 38, 39, 40 and 41.
  • the lines 40 and 41 are only briefly indicated in the figure.
  • the burners are arranged in the gasification reactor 27 symmetrically in one plane in such a way that there are two burners facing each other. In practice, the number and arrangement of the burners can of course also differ from the present example.
  • the raw gas obtained being cooled in the waste heat boiler 28, which is combined with the gasification reactor 27 to form a unit, and then fed to the line 42 of the gas treatment plant 29 .
  • This is where the raw gas is converted into synthesis gas, which can be drawn off via line 43 and used for further use.
  • the allocation container 8 is designed taking into account the generally known ones and those specially used for them Fuel determined data in such a way that a complete and uniform emptying via line 36 is ensured without the additional addition of conveying gas into this line.
  • the mass flow during the conveyance of the coal dust from the feed container 8 to the individual burners of the gasification reactor 27 depends on the set and automatically adjusted differential pressure between the feed container 8 and the gasification reactor 27. The details of this differential pressure control have already been discussed above.
  • the gas drawn off via line 26 is therefore first freed of the entrained coal dust in filter 50 and then passes via lines 51 and 52 into the quench part of the gasification reactor 27 or the gas treatment system 29.
  • the amount of gas via line 26 from the Allotment container 8 withdrawn gas is regulated by valve 49 in line 51.
  • the inventive recirculation of this gas into the gasification reactor 27 or the gas treatment system 29 ensures that no synthesis gas gets into the inert gas path of the pressure pot conveyors 3a and 3b and the cyclone filters 2a and 2b. This ensures the recovery of the CO2 used as an inert pumping medium used in these units, and pollution of the environment by expelling a non-inert pumping gas via line 22 is avoided.
  • fresh CO2 has to be introduced into the process, it is supplied via line 53 after appropriate compression.
  • the CO2 separated from the raw gas in the gas treatment plant 29 can also be used.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Air Transport Of Granular Materials (AREA)
  • Industrial Gases (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
EP89101155A 1988-03-26 1989-01-24 Procédé et installation de transport pneumatique d'un combustible finement granulé jusqu'à pulvérulent dans un réacteur de gazéification sous pression élevée Expired - Lifetime EP0335071B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3810404A DE3810404A1 (de) 1988-03-26 1988-03-26 Verfahren und vorrichtung zum pneumatischen foerdern eines feinkoernigen bis staubfoermigen brennstoffes in einen unter erhoehtem druck stehenden vergasungsreaktor
DE3810404 1988-03-26

Publications (2)

Publication Number Publication Date
EP0335071A1 true EP0335071A1 (fr) 1989-10-04
EP0335071B1 EP0335071B1 (fr) 1991-10-23

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Family Applications (1)

Application Number Title Priority Date Filing Date
EP89101155A Expired - Lifetime EP0335071B1 (fr) 1988-03-26 1989-01-24 Procédé et installation de transport pneumatique d'un combustible finement granulé jusqu'à pulvérulent dans un réacteur de gazéification sous pression élevée

Country Status (9)

Country Link
EP (1) EP0335071B1 (fr)
JP (1) JPH03128990A (fr)
DE (2) DE3810404A1 (fr)
ES (1) ES2027044T3 (fr)
GR (1) GR3003259T3 (fr)
IN (1) IN170974B (fr)
PL (1) PL156479B1 (fr)
TR (1) TR26352A (fr)
ZA (1) ZA889517B (fr)

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0447632A1 (fr) * 1990-02-16 1991-09-25 Krupp Koppers GmbH Procédé pour faire fonctionner une installation de gazéification de combustibles solides
WO2008132071A2 (fr) * 2007-04-30 2008-11-06 Siemens Aktiengesellschaft Utilisation d'un mélange de dioxyde de carbone et d'azote comme gaz d'inertisation et de transport dans des systèmes d'alimentation en poussière pour la gazéification sous pression de poussière de charbon
WO2008132072A2 (fr) * 2007-04-30 2008-11-06 Siemens Aktiengesellschaft Utilisation conjointe de dioxyde de carbone et d'azote dans un composant d'un système d'alimentation en poussière pour la gazéification sous pression de poussière de charbon
WO2008132069A2 (fr) * 2007-04-30 2008-11-06 Siemens Aktiengesellschaft Utilisation de dioxyde de carbone pur comme gaz d'inertisation et de transport dans des systèmes d'alimentation en poussière pour la gazéification sous pression de poussière de charbon
WO2009109297A2 (fr) * 2008-03-05 2009-09-11 Uhde Gmbh Système de réacheminement dans un réacteur de gazéification du charbon
WO2010056334A2 (fr) * 2008-11-12 2010-05-20 Exxonmobil Research And Engineering Company Système d'injection de gazéifieur
WO2010086008A3 (fr) * 2009-01-28 2010-11-11 Uhde Gmbh Procédé pour alimenter un réacteur de gazéification à lit entraîné en combustible prélevé dans un réservoir
WO2010066334A3 (fr) * 2008-12-09 2010-11-18 Uhde Gmbh Processus et installation pour alimenter un réacteur servant à produire un gaz de synthèse brut
CN103318648A (zh) * 2013-06-28 2013-09-25 中冶南方工程技术有限公司 转炉煤气干法除尘粗灰气力输送方法
CN103332458A (zh) * 2013-06-28 2013-10-02 中冶南方工程技术有限公司 一种转炉煤气干法除尘细灰气力输送系统
CN103332494A (zh) * 2013-06-28 2013-10-02 中冶南方工程技术有限公司 一种转炉一次烟气干法除尘粗灰气力输送方法
CN103332490A (zh) * 2013-06-28 2013-10-02 中冶南方工程技术有限公司 转炉煤气干法除尘细灰气力输送系统
FR3013232A1 (fr) * 2013-11-21 2015-05-22 Commissariat Energie Atomique Dispositif de transfert de materiau granulaire a consommation d'energie reduite
EP1934311B1 (fr) 2005-10-14 2016-07-27 Shell Internationale Research Maatschappij B.V. Procédé de production de gaz de synthèse ou d'hydrocarbures

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4102965C2 (de) * 1991-02-01 1999-09-09 Krupp Koppers Gmbh Vorrichtung und Verfahren zum Fördern eines feinkörnigen bis staubförmigen Brennstoffes in einen unter erhöhtem Druck stehenden Vergasungsreaktor
JP5651440B2 (ja) * 2010-11-22 2015-01-14 バブコック日立株式会社 石炭ガス化発電プラントの石炭搬送システム
JP2012162660A (ja) * 2011-02-08 2012-08-30 Babcock Hitachi Kk 石炭ガス化石炭搬送システム及び石炭ガス化複合発電プラント
CN102925216A (zh) * 2012-10-25 2013-02-13 云南煤化工集团有限公司 一种加压气化炉煤锁间互相充泄压的方法

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2059377A (en) * 1979-09-22 1981-04-23 Saarbergwerke Ag A method of pneumatically conveying fine-grain fuel to a gasifier
GB2103387A (en) * 1981-07-17 1983-02-16 Freiberg Brennstoffinst A method of regulating mass flow
EP0101098A2 (fr) * 1982-06-23 1984-02-22 Shell Internationale Researchmaatschappij B.V. Procédé pour transporter un combustible solide finement divisé
DD161080A1 (de) * 1978-09-28 1984-10-10 Brennstoffinstitut Freiberg 92 Verfahren und vorrichtung zum vergasen von festen brennstoffen
DE3509221A1 (de) * 1984-03-16 1985-09-19 Shell Internationale Research Maatschappij B.V., Den Haag Vorrichtung fuer die vergasung eines pulverisierten festen brennstoffes

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DD161080A1 (de) * 1978-09-28 1984-10-10 Brennstoffinstitut Freiberg 92 Verfahren und vorrichtung zum vergasen von festen brennstoffen
GB2059377A (en) * 1979-09-22 1981-04-23 Saarbergwerke Ag A method of pneumatically conveying fine-grain fuel to a gasifier
GB2103387A (en) * 1981-07-17 1983-02-16 Freiberg Brennstoffinst A method of regulating mass flow
EP0101098A2 (fr) * 1982-06-23 1984-02-22 Shell Internationale Researchmaatschappij B.V. Procédé pour transporter un combustible solide finement divisé
DE3509221A1 (de) * 1984-03-16 1985-09-19 Shell Internationale Research Maatschappij B.V., Den Haag Vorrichtung fuer die vergasung eines pulverisierten festen brennstoffes

Cited By (34)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0447632A1 (fr) * 1990-02-16 1991-09-25 Krupp Koppers GmbH Procédé pour faire fonctionner une installation de gazéification de combustibles solides
EP1934311B1 (fr) 2005-10-14 2016-07-27 Shell Internationale Research Maatschappij B.V. Procédé de production de gaz de synthèse ou d'hydrocarbures
EP1934311B2 (fr) † 2005-10-14 2020-07-15 Air Products And Chemicals, Inc. Procédé de production d'hydrocarbures
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CN103332458B (zh) * 2013-06-28 2015-09-02 中冶南方工程技术有限公司 一种转炉煤气干法除尘细灰气力输送系统
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PL156479B1 (en) 1992-03-31
JPH03128990A (ja) 1991-05-31
ES2027044T3 (es) 1992-05-16
IN170974B (fr) 1992-06-27
GR3003259T3 (en) 1993-02-17
DE3810404A1 (de) 1989-10-12
TR26352A (tr) 1994-02-10
DE58900390D1 (de) 1991-11-28
PL278445A1 (en) 1989-11-13
ZA889517B (en) 1989-09-27
EP0335071B1 (fr) 1991-10-23

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